US20200181044A1 - Process and facility for producing propylene by combining propane dehydrogenation and a steam cracking method with propane recirculation into the steam cracking method - Google Patents

Process and facility for producing propylene by combining propane dehydrogenation and a steam cracking method with propane recirculation into the steam cracking method Download PDF

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US20200181044A1
US20200181044A1 US16/630,361 US201816630361A US2020181044A1 US 20200181044 A1 US20200181044 A1 US 20200181044A1 US 201816630361 A US201816630361 A US 201816630361A US 2020181044 A1 US2020181044 A1 US 2020181044A1
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propane
component mixture
steps
separation
separation step
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Torben Höfel
Christine TÖGEL
Mathieu Zellhuber
Heinrich Laib
Stefan Kotrel
Martin Dieterle
Florina Corina Patcas
Sonja Giesa
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Linde GmbH
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Linde GmbH
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    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/327Formation of non-aromatic carbon-to-carbon double bonds only
    • C07C5/333Catalytic processes
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24Stationary reactors without moving elements inside
    • B01J19/245Stationary reactors without moving elements inside placed in series
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00Purification; Separation; Use of additives
    • C07C7/005Processes comprising at least two steps in series
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00Purification; Separation; Use of additives
    • C07C7/04Purification; Separation; Use of additives by distillation
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00Purification; Separation; Use of additives
    • C07C7/09Purification; Separation; Use of additives by fractional condensation
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002Chemical plants
    • B01J2219/00027Process aspects
    • B01J2219/0004Processes in series
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10Feedstock materials
    • C10G2300/1037Hydrocarbon fractions
    • C10G2300/104Light gasoline having a boiling range of about 20 - 100 °C
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10Feedstock materials
    • C10G2300/1081Alkanes
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40Characteristics of the process deviating from typical ways of processing
    • C10G2300/4056Retrofitting operations
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20C2-C4 olefins

Definitions

  • the present invention relates to a process and a plant for the production of propylene and to a process for retrofitting a steam cracking plant according to the preambles of the independent claims.
  • Propylene (propene) is traditionally produced mainly by steam cracking of hydrocarbon feedstocks and other conversion methods in refinery processes. In these cases propylene is a minor by-product. Due to the increasing demand for propylene, especially polypropylene, propane dehydrogenation is also used.
  • Propane dehydrogenation is a well-known method in the petrochemical industry and is described in the article “Propene” in Ullmann's Encyclopedia of Industrial Chemistry, Online Edition 16 Sep. 2013, DOI: 10.1002/14356007.a22_211.pub3, in particular in Section 3.3.1, “Propane dehydrogenation”.
  • Propane dehydrogenation is an endothermic equilibrium reaction generally carried out on noble or heavy metal catalysts, such as platinum or chromium.
  • the dehydrogenation reaction is highly selective. For commercially available processes, total yields of approx. 90% are cited. Notwithstanding this high selectivity, smaller quantities of hydrocarbons with one, two, four and more than four carbon atoms are typically produced as by-products in addition to the hydrogen which is cleaved off. These by-products must be separated from the target product propylene.
  • the purification of a component mixture produced during propane dehydrogenation can at least partly be carried out together with the purification of a component mixture containing propylene from another method in which propylene is formed, e.g. a steam cracking method or a refinery process.
  • WO 2015/128039 A1 describes that a component mixture with predominantly or exclusively two carbon atoms, which is formed in a common separation, to which a component mixture formed using the propane dehydrogenation method and a component mixture formed using the steam cracking method are subjected, is returned to the steam cracking method.
  • a component mixture with three or more carbon atoms formed in the joint separation is returned to the propane dehydrogenation method because it contains considerable amounts of propane.
  • Other publications also reveal a return of propane or mixtures of components containing propane to a propane dehydrogenation method.
  • the present invention has the task of improving and making more efficient processes for the production of propylene, in which a component mixture is purified from a propane dehydrogenation method and in which certain components or fractions are recycled, if an additional steam cracking method is available.
  • the present invention proposes a process and plant for the production of propylene and a process for retrofitting a plant to perform a steam cracking method with the respective characteristics of the independent claims.
  • Preferred embodiments are the subject of the dependent claims as well as the following description.
  • the present invention recognizes that paradoxically, recycling a separation product predominantly containing propane not to the propane dehydrogenation method but to the other propane production method is advantageous when the separation product predominantly containing propane is formed in a separation to which at least a portion of a first component mixture provided using a propane dehydrogenation method and optionally also at least a portion of a second component mixture provided using a further propane production method are subjected.
  • the other propane production method is a steam cracking method.
  • Propane-containing feeds for propane dehydrogenation are typically present with a high propane concentration (e.g. at least 94 percent by volume propane and in each case at most 4 percent by volume butane, 3 percent by volume ethane, and 0.1 percent by volume olefins).
  • a separation product from a separation which mainly contains propane in particular if to this joint separation is also subjected a component mixture which is provided using a steam cracking method, may be of inferior quality. This applies at least if the separation does not involve a disproportionate effort in terms of the purity of the products obtained.
  • a corresponding separation product predominantly containing propane therefore contains olefins, in particular mono- and polyunsaturated olefins with three carbon atoms and mono- and polyunsaturated olefins with four carbon atoms.
  • the reactor or its catalyst used may have extremely small tolerances with respect to components such as methyl acetylene, propadiene and butadiene, which are regularly formed in corresponding other propylene production methods, in particular in steam cracking methods.
  • a recycle to the propane dehydrogenation method would therefore require at least extensive separation of the above components in order to comply with the tolerances of an appropriate reactor. However, this would entail a disproportionately high level of technical and procedural effort.
  • a process according to a particularly preferred embodiment of the invention comprises a combined purification or separation of component mixtures from the propane dehydrogenation method and the steam cracking method.
  • the process according to the invention can basically also be carried out without a combined purification or separation.
  • the respective component mixtures contain identical or similar components, i.e. the component mixtures do not “contaminate” each other with certain components not contained in the respective other component mixture (e.g. with hydrogen, carbon dioxide or oxygenates).
  • a combination of purification is particularly advantageous if the respective component mixtures have a similar concentration range, so that a synergetic separation process can be expected. However, this is normally not the case in practice. Furthermore, a combination of purification is advantageous if one of the processes supplies significantly smaller quantities of a corresponding component mixture or if a corresponding plant is smaller and therefore separate purification is not worthwhile. This may be the case in particular if the other propylene production method, e.g. a steam cracking method, is already implemented in the form of a plant and a propane dehydrogenation method with significantly lower capacity is retrofitted to increase the propylene product capacity. This could be particularly advantageous if some plant components for the steam cracking method are no longer running at full capacity due to a later change in use and these capacities can be used by the propane dehydrogenation method.
  • a steam cracking method e.g. a steam cracking method
  • the steam cracking method is already designed for the use of a propane-containing feed, this can also be continued to be operated after retrofitting with propane.
  • the steam cracking method receives at least part of the separation product, which mainly contains propane, which does not have a major effect on the process.
  • the propane dehydrogenation method obtains the higher quality propane feedstock from another source (and possibly also at least part of the separation product predominantly containing propane).
  • the (common) separator does not have to be designed to meet the requirements of the propane dehydrogenation method with respect to the separation product predominantly containing propane, i.e. in particular no steps for (separate) hydrogenation and no steps for the separation of hydrocarbons with four or more carbon atoms are required in order to comply with the tolerances of the propane dehydrogenation method.
  • One possibility for advantageously designing the preferred embodiment of the present invention, in which a combined purification or separation is used, is therefore to pretreat a first component mixture, which is obtained using the propane dehydrogenation method, in such a way that it is present in a state depleted of (at least) hydrogen and in particular at an increased pressure.
  • the first component mixture is subjected to one or more pre-separation steps, which are subsequently referred to as the “first” pre-separation steps.
  • the component mixture pre-treated in this way which is subsequently referred to as the “third” component mixture, contains mainly hydrocarbons with three carbon atoms due to its pre-treatment. It may also contain smaller quantities of methane, residual hydrogen and hydrocarbons containing two carbon atoms and hydrocarbons containing four carbon atoms and, where appropriate, more than four carbon atoms.
  • pretreat a second component mixture which is obtained using the steam cracking method, in such a way that it is present in a state depleted (at least) of hydrogen and methane and, in particular, also at an increased pressure.
  • the second component mixture is subjected to one or more pre-separation steps, which are subsequently also referred to as “second pre-separation steps”.
  • the component mixture pretreated in this way which is hereinafter referred to as the “fourth” component mixture if specifically referred to here, advantageously contains, due to its pre-treatment, predominantly hydrocarbons similar to those contained in the third component mixture and in a comparable concentration range, as well as comparable quantities of residual hydrogen and residual methane, unless completely separated.
  • a depletion of hydrocarbons with two carbon atoms can also take place in the course of the depletion of hydrogen and methane in the course of the second preliminary separation step or steps.
  • a Demethanizer First process or a Deethanizer First process can be used in the course of the second pre-separation step or steps.
  • the use of a Depropanizer-First process is also possible in principle. Further details are explained below. However, even in the course of the first preliminary separation step or steps, a depletion of hydrocarbons with two carbon atoms can take place if this is appropriate. Further aspects of these embodiments are explained below.
  • composition and pressure of the third and fourth component mixtures which have been at least partially adjusted to each other by the first pre-separation step or steps and by the second pre-separation step or steps, can be combined in a particularly advantageous manner and subsequently subjected to subsequent common separation steps. This makes it possible to design corresponding plant components for both processes together and thus to build a corresponding plant with lower investment costs and/or to operate it with lower operating costs.
  • a component mixture compared to another component mixture here especially the third compared to the first and the fourth compared to the second, at one or more components, here especially at hydrogen or hydrogen and methane “depleted” is understood to mean that the depleted component mixture contains at most 0.5 times, 0.2 times, 0.1 times, 0.01 times or 0.001 times the content of the one or more components relative to the nondepleted component mixture and on a molar, mass or volume basis. Also a complete distance, i.e. a “depletion to zero” is understood here as a depletion.
  • the term “predominantly” refers to a content of at least 60%, 80%, 90%, 95% or 99% on a molar, mass or volume basis.
  • the present invention proposes a process for the production of propylene which involves carrying out a propane dehydrogenation method to obtain a first component mixture which contains at least hydrogen, ethane, ethylene, propane and propylene, and carrying out a further propylene production method, in particular a steam cracking method, to obtain a second component mixture which contains at least hydrogen, methane, ethane, ethylene, propane and propylene.
  • a propane dehydrogenation method is advantageously supplied with inserts containing propane and the steam cracking method with inserts rich in hydrocarbons.
  • the latter are, for example, naphtha, but may also be lighter or heavier applications, i.e. those which contain hydrocarbons with a lighter and/or heavier boiling point than are typically present in naphtha.
  • a separation product predominantly containing propane is formed using at least part of the propane of the first component mixture and one or more propane separation steps.
  • the separation product predominantly containing propane can also be formed by using at least part of the propane of the second component mixture, i.e. by a common purification or separation.
  • the propane separation step or steps may include in particular the use of a C3 splitter from which a separation product predominantly or exclusively containing propylene can be removed at the head and the separation product predominantly containing propane can be removed at the bottom.
  • a C3 splitter is typically preceded by further separation steps, as explained below.
  • the feed of a corresponding C3 splitter can typically be taken from a so-called depropanizer or a corresponding depropanizer column, as is also generally known from the cited technical literature.
  • a depropanizer is a rectification column from which a gaseous fraction containing predominantly or exclusively hydrocarbons with three carbon atoms can be withdrawn at the top and a liquid fraction containing predominantly or exclusively hydrocarbons with four and optionally more carbon atoms can be withdrawn at the bottom. From other apparatuses assigned to a corresponding rectification column which are part of a corresponding depropanizer, such as absorbers, such fractions can also be removed instead of the rectification column itself or in addition to it.
  • a corresponding depropanizer may be arranged at different locations in a separation sequence for processing a component mixture, in particular a component mixture obtained by a steam cracking method or another propane production process.
  • a corresponding depropanizer can be arranged downstream of a deethanizer or a corresponding deethanizer column within the scope of the present invention and set up for the separation processing of a bottom product of the deethanizer.
  • a deethanizer can be used in the course of the present invention in the course of the second pre-separation step or steps or already in the course of the propane separation step or steps, depending on whether a deethanizer-first process or a demethanizer-first process is used.
  • a depropanizer which can also be at the first position of a corresponding separation sequence.
  • At least part of the first component mixture and, in accordance with the design with common purification or separation, at least part of the second component mixture is always added to the propane separation step or steps used in the context of the present invention.
  • at least part it shall also be understood that a fraction formed, for example, in the pre-separation step or steps described above, is added to the propane separation step or steps.
  • a “part” does not have to be a partial amount with identical composition, but a “part” may also be a fraction with a different composition, in particular another mixture of components formed in a pre-separation step (first or second) already mentioned.
  • At least a part (in terms of a partial amount) of the first component mixture and optionally at least a part (in terms of a partial amount) of the second component mixture can be supplied to the propane separation step or steps used in the present invention, but it is also possible to supply to the propane separation step or steps one or more component mixtures (namely in particular the already mentioned “third” and “fourth” component mixtures) formed using at least a part of the first component mixture and at least a part of the second component mixture.
  • the separation product predominantly containing propane is “at least partly” returned to the further propylene production method
  • this also includes a constellation according to which part of the separation product predominantly containing propane is returned to the further propylene production method and another part of the separation product predominantly containing propane is returned to the propane dehydrogenation method.
  • the separation product which mainly contains propane, can be admixed here to the extent that it does not interfere with the propane dehydrogenation method.
  • the remainder of the separation product which mainly contains propane, can, however, be returned to the further propylene production method.
  • the separation product predominantly containing propane is not returned to the propane dehydrogenation method, so that the propane dehydrogenation method in this design of the process conforming to the invention is supplied only with propane which does not originate from either the first or the second component mixture.
  • the present invention does not require time-consuming cleaning due to the return of the separation product, which mainly contains propane.
  • a separation product containing only predominantly propane may be used, which may contain from 0.1 to 25% by volume of monounsaturated and polyunsaturated hydrocarbons, in particular monounsaturated and polyunsaturated hydrocarbons containing three and four carbon atoms, in particular propadiene and butadiene.
  • Such a separation product can be tolerated within higher limits in another propylene production method, in particular a steam cracking method, than in the propane dehydrogenation method.
  • a process according to a particularly preferred embodiment of the present invention also includes the formation of a separation product containing predominantly or exclusively propylene using at least part of the problem of the first and second component mixture and using the propane separation step or steps.
  • a C3 splitter can be used in this context.
  • the present invention further comprises, in the embodiment just described, the formation of a separation product predominantly or exclusively containing ethylene using at least part of the ethylene of the first and second component mixtures and using one or more further separation steps, and the formation of a separation product predominantly or exclusively containing ethane using at least part of the ethane of the first and second component mixtures and using the further separation step or steps.
  • the further separation step or steps typically include the use of a so-called C2 splitter, from which the separation product predominantly or exclusively containing ethylene can be taken at the top and the separation product predominantly or exclusively containing ethane can be taken at the bottom.
  • a corresponding C2 splitter can in particular be fed with a fraction containing predominantly or exclusively ethane and ethylene which can be withdrawn from the head of a deethanizer, i.e. a corresponding rectification column or an apparatus associated therewith, in a demethanizer first process and from the bottom of a demethanizer in a deethanizer first process.
  • a deethanizer i.e. a corresponding rectification column or an apparatus associated therewith
  • the present invention comprises pre-separation steps according to particularly preferred embodiments, wherein it is provided that at least a part of the first component mixture is subjected to one or more first pre-separation steps to obtain a third component mixture, which comprises a pressure increase and an at least partial removal of hydrogen, and that at least a part of the second component mixture is subjected to one or more second pre-separation steps to obtain a fourth component mixture, which comprises a pressure increase, an at least partial removal of hydrogen and an at least partial removal of methane.
  • a deethanizer-first method otherwise in connection with a demethanizer-first method.
  • this invention can also be used in conjunction with a Depropanizer-First process.
  • the present invention provides, in accordance with the embodiments described above, that at least part of the third component mixture, together with at least part of the fourth component mixture, is subjected to the propane separation step or steps in an alternative.
  • at least part of the third component mixture together with the second component mixture is subjected to the second pre-separation step or steps to form the fourth component mixture and that the fourth component mixture is subjected to the propane separation step or steps.
  • the third and fourth component mixtures can be “parts” of the first and second component mixtures, respectively, in the sense explained above.
  • the present invention with its respective embodiments explained below, provides different possibilities for combining the third component mixture with the fourth component mixture or the respective proportions used. In all cases, the main advantage of the present invention is that a particularly simple and efficient joint separation is possible due to a comparable composition of the third and fourth component mixtures.
  • this invention can be used in conjunction with a deethanizer-first process.
  • ethane and ethylene are also at least predominantly removed, so that these do not predominantly transition from the second to the fourth component mixture or corresponding proportions.
  • the fourth component mixture can also be a liquid that is present on a separating tray near the bottom of a corresponding rectification column.
  • a “separating tray near the bottom” is a separating tray arranged in the lower half, especially in the lower third, in the lower quarter or in the lower fifth of the rectification column.
  • a “rectification column” is a separation unit which is set up to at least partially separate one or more gaseous or liquid component mixtures, or in the form of a two-phase mixture with liquid and gaseous components, possibly also in the supercritical state, by rectification, i.e. to produce pure substances or at least component mixtures with a different composition from the component mixture(s). Rectification is known to involve repeated evaporation and condensation processes, especially on or using suitable internals such as separating trays or ordered or disordered packings.
  • a rectification column for use within the scope of this invention has a bottom evaporator.
  • a rectification column for use in the context of the present invention also contains a head condenser which condenses gas rising in the rectification column and returns it to the rectification column in a condensed state.
  • separation processes specifically used for the treatment of component mixtures formed by steam cracking in particular separation processes involving demethanization and deethanization, reference is made to the already cited article “Ethylene” in Ullmann's Encyclopedia of Industrial Chemistry.
  • Such separation processes differ in particular in the sequence of the respective separation steps.
  • the demethanizer first process also known as the front-end demethanizer process
  • the deethanizer first process also known as the front-end deethanizer process
  • the depropanizer first process also known as the front-end depropanizer process
  • this invention is particularly suitable for use in conjunction with the deethanizer first method, but also for use with the demethanizer first method or the depropanizer first method.
  • demethanizers, deethanizers and depropanizers may be designed as corresponding rectification columns or may include such rectification columns, which are hereinafter also referred to as demethanization columns, deethanization columns or depropanization columns.
  • demethanizers deethanizers
  • depropanizers are understood to mean arrangements with corresponding rectification columns, to which, however, additional apparatuses, such as absorbers in deethanizers, can also be assigned. The same applies if there is talk of “demethanization”, “deethanization” or “depropanization”.
  • fractions “from the head” or “from the bottom” can be withdrawn from demethanizers, deethanizers and depropanizers or corresponding rectification columns, these can also be withdrawn alternatively or in addition to the rectification column from the head or from the bottom of corresponding assigned apparatus.
  • the removal of hydrogen and methane in the second pre-separation step or steps also removes ethane and ethylene at least predominantly, i.e. a deethanizer-first process is carried out.
  • Hydrogen and methane are removed in the second pre-separation step or steps, in which ethane and ethylene are also at least predominantly removed, using a deethanization column.
  • the fourth component mixture occurs in the area of a tray near the bottom of such a deethanization column.
  • a corresponding liquid is depleted of hydrogen, methane and hydrocarbons with two carbon atoms or corresponding components have been removed to a large extent.
  • a second advantageous embodiment is also possible in which ethane and ethylene are at least predominantly not removed during the removal of hydrogen and methane in the second pre-separation step or steps. Ethane and ethylene are therefore at least predominantly transferred to the fourth component mixture in these versions of the invention.
  • a demethanizer first method is used. If a corresponding rectification column is used to remove hydrogen and methane, the fourth component mixture is in particular a bottom liquid of such a rectification column.
  • the removal of hydrogen and methane in the second pre-separation step or steps, in which ethane and ethylene are at least predominantly not removed, can therefore be carried out using a demethanization column.
  • a component mixture predominantly or exclusively containing hydrogen and methane is taken from the head of such a demethanization column or an apparatus associated with it, and a bottom liquid predominantly or exclusively containing hydrocarbons with two or more carbon atoms can be withdrawn from the bottom. This bottom liquid can in particular subsequently be deethanized, as explained below.
  • a deethanization column in addition to the demethanization column, a deethanization column is foreseen.
  • the third component mixture can be fed in particular into a bottom or a separation tray near the bottom of the demethanization column or into the lower area, i.e. the area of a separation tray near the bottom of the deethanization column.
  • the third component mixture can be fed into the bottom area of the deethanization column in particular.
  • depropanization columns are also used.
  • the third component mixture can also be fed into a depropanization column. The same applies if a depropanizer-first method is used. In this case, the third component mixture can also be fed into the depropanization column.
  • the hydrogen content of the first component mixture is depleted to a value of 0 to 10 mol %, in particular 0.1 to 5 mol %, for example 0.2 to 2 mol %, within the framework of the present invention in the context of the first pre-separation step or steps of the first component mixture.
  • the second component mixture can also be fed to a common separation, since its other composition is sufficiently similar to a corresponding fluid from a steam cracking method. As mentioned, any remaining hydrogen can simply be removed.
  • the first pre-separation step or steps to which the first component mixture is subjected also include an increase in pressure, in particular to an absolute pressure of 3 to 40 bar, in particular 10 to 30 bar, for example 12 to 30 bar.
  • the pressure level depends on a pressure level at which a demethanizer or deethanizer or depropanizer is operated, as it is used in the second pre-separation step or steps, i.e. the pressure increase also carried out there takes place within the scope of the second pre-separation step or steps. Therefore, the pressure levels of the third and fourth component mixtures can be adjusted in this way in a particularly advantageous way.
  • Hydrogen depletion as part of the pretreatment of the first component mixture or its part subjected to the pretreatment may include in particular a partial condensation of hydrocarbons with three carbon atoms after the pressure increase or compression described above. In this way, a fraction is formed which predominantly contains hydrocarbons with three carbon atoms, but into which the other components mentioned can also partially pass. In any case, this fraction is depleted of hydrogen compared to the first component mixture.
  • condensation is particularly advantageous because, as explained below, it can be carried out at least in part within the framework of this invention using refrigeration, which can be provided by process streams present in the process.
  • partial condensation may be carried out using refrigeration, which may be obtained at least in part by decompressing a stream predominantly containing propane.
  • This stream which mainly contains propane, may, for example, be the second separation product formed in the first separation step or steps.
  • This second separation product can be expanded to produce cold and then returned to the process, in particular the propane dehydrogenation method or the steam cracking method.
  • first component mixture or its portion subject to the first pre-separation step or steps can be fed to the first pre-separation step or steps in the form of a stream of material which is compacted and a partial stream of which is expanded downstream of compaction.
  • the relaxed partial flow can be fed back into the compression process, so that cold can be generated continuously.
  • cold box processes as they are generally known from the state of the art, or processes based on other separation principles can also be used in the context of this invention.
  • the propane dehydrogenation method is carried out under water-free conditions and/or in the complete absence of oxygen (also in covalently bound form and/or during regeneration).
  • oxygen also in covalently bound form and/or during regeneration.
  • the first component mixture can, without separating water and carbon dioxide during the formation of the third component mixture, be fed to a rectification column, for example, which serves to deethanize and which is typically operated at cryogenic temperatures at which water and carbon dioxide would freeze out.
  • a rectification column for example, which serves to deethanize and which is typically operated at cryogenic temperatures at which water and carbon dioxide would freeze out.
  • feeding the third component mixture after the first separation step or steps to the first separation step or steps in which the third component mixture is combined with the fourth component mixture or a component mixture formed therefrom is/are particularly advantageous if the respective compositions are identical or do not differ by more than a predetermined extent.
  • a hydrogen content in the third component mixture differs from a hydrogen content in the fourth component mixture by not more than 50%, in particular by not more than 25%, for example by not more than 10%, of a hydrogen content in the third component mixture and if a content of hydrocarbons having three carbon atoms, in particular propylene, in the third component mixture differs from a content of hydrocarbons having three carbon atoms, in particular propylene, in the fourth component mixture by not more than 50%, in particular by not more than 25%, for example by not more than 10%.
  • the present invention further extends to a plant for the production of propylene, having a first reactor unit which is provided and arranged to carry out a propane dehydrogenation method to obtain a first component mixture which contains at least hydrogen, ethane, ethylene, propane and propylene, a second reactor unit which is provided and arranged to carry out a further propylene production method, in particular a steam cracking method, to obtain a second component mixture which contains at least hydrogen, methane, ethane, ethylene, propane and propylene, and a first separation unit provided and arranged to form a separation product predominantly containing propane using at least a portion of the propane of the first and, according to a preferred execution form also the second component mixture and using one or more first separation steps, wherein means are provided arranged to supply at least a portion of the first component mixture and, according to the preferred embodiment also at least a portion of the second component mixture to the propane separation step or steps.
  • such a plant is characterised by means which are made available and set up to return the separation product, which mainly contains propane, at least in part to the further propylene production method.
  • the invention further comprises a process for retrofitting a plant adapted to perform a steam cracking method using a plurality of plant components such as cracking furnaces, processing equipment and separating apparatus, wherein a hydrocarbon-containing feed mixture having a first composition is fed to the plant prior to retrofitting.
  • the retrofitting comprises adding a hydrocarbon-containing feed mixture with a second, different composition to the plant instead of the hydrocarbon-containing feed mixture with the first composition, and using one or more of the plant components for a propane dehydrogenation method instead of for the steam cracking method, i.e. reallocating freed capacities accordingly.
  • An example of this is a change in the feedstock mix of the steam cracking method from heavier hydrocarbons, for example predominantly naphtha, to lighter hydrocarbons, for example ethane and/or propane and butane.
  • lighter hydrocarbons for example ethane and/or propane and butane.
  • plant components for processing the entire product gas such as the raw gas compressor, and plant components for processing the light product fraction, such as the demethanizer, are likely to be subjected to the same or even higher loads than before after the change in the feed mixture
  • other plant components for example for processing heavier product fractions, are likely to be relieved.
  • These relieved plant components can include the depropanizer as well as all plant components for processing a fraction of hydrocarbons with three carbon atoms including hydrogenation and a splinter.
  • a process as described above is carried out after the retrofit and/or a corresponding plant is provided by means of the retrofit.
  • the advantage mentioned at the beginning can be achieved that the corresponding products of a propane dehydrogenation can be purified together with the products of the steam cracking method and separate purification can be dispensed with.
  • FIG. 1 illustrates a process designed according to an embodiment of the invention in a highly simplified, schematic representation.
  • FIG. 1 illustrates a process designed according to the invention in a highly simplified, schematic representation and is designated 10 in total.
  • Process 10 comprises a process 1 for propane dehydrogenation, a steam cracking method 2 , one or more first preliminary separation steps V 1 , one or more second preliminary separation steps V 2 , and one or more propane separation steps S 1 .
  • the first pre-separation step or steps V 1 , the second pre-separation step or steps V 2 , the propane separation step or steps S 1 and any other separation steps not separately illustrated here can be grouped as required and, for example, combined in corresponding plant components.
  • procedure 1 for propane dehydrogenation is supplied with an initial input stream E 1 , which may include propane in particular, but not recycled propane.
  • the first input current E 1 is formed exclusively using an output current E 0 , which is fed to process 10 from the BL system limit.
  • a part of this output stream E 0 can also be fed to the steam cracking method 2 , as illustrated in the form of a dashed material stream E 0 ′.
  • the first input stream E 1 is divided into two partial streams E 1 ′ and E 1 ′′, wherein the partial stream E 1 ′ is fed directly to process 1 for propane dehydrogenation and the partial stream E′′ is first used in the first pre-separation step or steps V 1 .
  • the partial stream E 1 ′′ can, for example, be expanded to generate cold and only then fed into process 1 for propane dehydrogenation.
  • the input stream E 1 can also be treated completely as illustrated here with regard to the partial stream E 1 ′, i.e. it can be fed directly to process 1 for propane dehydrogenation.
  • Process 1 for propane dehydrogenation is carried out in a generally known manner so that a first component mixture A containing at least hydrogen, ethane, ethylene, propane and propylene is formed therein and which can be carried out from process 1 for propane dehydrogenation in the form of a corresponding material stream.
  • Procedure 1 for propane dehydrogenation may in particular be carried out using one or more suitable reactors, which may have been designed in a customary manner.
  • the first component mixture A or the corresponding material flow is at least partially fed to the first pre-separation step or steps V 1 in which the first component mixture A or the corresponding material flow is subjected to a pressure increase and at least partial removal of hydrogen.
  • this can be done in a generally known way.
  • the first component mixture A or the corresponding material flow can be liquefied in the first pre-separation step or steps V 1 .
  • Separated hydrogen is illustrated in the form of a material stream called H 2 .
  • H 2 a material stream called H 2 .
  • an at least partial removal of hydrocarbons with two carbon atoms is possible, but optional, as not shown separately in FIG. 1 .
  • a component mixture is obtained, which is also referred to here as the third component mixture C, and which can be executed in the form of a corresponding material flow from the first pre-separation step or steps V 1 .
  • Possible hydrogen contents of the third component mixture C or the corresponding material flow have already been explained above.
  • the third component mixture C downstream of the first preliminary separation step or steps V 1 still contains hydrocarbons with three carbon atoms and minor amounts of other components, for example hydrocarbons with two hydrocarbon atoms, if not yet removed, and hydrocarbons with four carbon atoms formed as by-products in propane dehydrogenation method 1 .
  • the first component mixture A also contains water and carbon dioxide, these can also be removed in the first pre-separation step or steps V 1 .
  • the steam cracking method 2 which can also be carried out in the usual manner, for example by using several cracking furnaces, is fed a hydrocarbon-rich feed in the form of a material flow E 2 in the example shown, which is fed from the BL plant boundary.
  • the hydrocarbon-rich use can include in particular naphtha and lighter hydrocarbons, but also heavy hydrocarbons.
  • hydrocarbon-rich applications may include paraffinic hydrocarbons with two, three and four carbon atoms, in particular ethane, propane and butane.
  • the steam cracking method 2 as a whole or different furnaces used in the steam cracking method 2 can also be supplied with different hydrocarbon feedstocks and processed there under different splitting conditions.
  • the steam cracking method 2 is additionally supplied with the aforementioned partial stream E 0 ′′ of the output stream E 0 , a propane-containing separation product P 2 of the propane separation step or steps S 1 and a further recirculated stream C 2 H 6 which contains predominantly or exclusively ethane.
  • the return of the separation product P 2 which mainly contains propane
  • the supply or return of the other flows shown is completely optional within the scope of this invention.
  • the hydrocarbons of the hydrocarbon-rich feed(s) are at least partially converted so that a second component mixture B is obtained which contains at least hydrogen, methane, ethane, ethylene, propane and propylene.
  • the second component mixture B can be drawn off from the steam cracking method 2 in the form of a corresponding material flow and then at least partly fed to one or more second pre-separation steps V 2 .
  • the composition of the second component mixture B or of the corresponding material flow depends to a large extent on the hydrocarbon-rich application supplied to the steam cracking method 2 .
  • the second pre-separation step or steps V 2 may include demethanization and/or deethanization in particular.
  • a demethanizer first process or a deethanizer first process can be used. Both variants have already been explained before and are generally known from the state of the art. They are therefore not explained here again.
  • the mentioned material stream C 2 H 6 which predominantly or exclusively contains ethane, as well as one or more product streams, here commonly designated PX, can also be formed in the second pre-separation step or steps.
  • the product flow(s) PX can be led to the BL system limit.
  • the hydrogen-rich material flow HZ can be combined with the hydrogen-rich material flow H 2 and led together with this to the BL plant boundary. Together with the hydrogen-rich material stream HZ, methane in particular can also be discharged.
  • a component mixture D is formed by the use of the second pre-separation step or steps V 2 , which is referred to here as the fourth component mixture, and which is at least depleted of hydrogen and methane with respect to the second component mixture B, or which is formed by at least partially removing hydrogen from methane from the second component mixture B.
  • the second component mixture B is formed by the use of the second pre-separation step or steps V 2 .
  • This fourth component mixture D is fed to the propane separation step or steps S 1 in which the separation product P 2 , which mainly contains propane, is formed.
  • a separation product P 1 containing predominantly or exclusively propylene can also be formed in the propane separation step or steps S 1 and taken to the BL plant boundary.
  • One or more further separation products herein referred to as PY, can also be separated in the propane separation step or steps S 1 and led to the plant boundary BL.
  • further separation steps such as deethanization or depropanization, may be part of the second pre-separation step or steps V 2 or part of the propane separation step or steps S 1 .
  • the third component mixture C can be fed to the second pre-separation step or steps V 2 and/or the propane separation step or steps S 1 .
  • the third component mixture can be in the region of a separating bottom near the bottom of a demethanization column or deethanization column used in the second preliminary separation step or steps V 2 and/or in a depropanization column which can be part of the second preliminary separation step or steps V 2 and or of the propane separation step or steps S 1 .
  • Corresponding alternatives are illustrated in the form of material flows C′ and C′′. Material flows can also be returned from the propane separation step or steps S 1 to the pre-separation step or steps V 2 , as illustrated here in the form of the material flow PZ.

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US16/630,361 2017-07-12 2018-07-12 Process and facility for producing propylene by combining propane dehydrogenation and a steam cracking method with propane recirculation into the steam cracking method Abandoned US20200181044A1 (en)

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EP17180984.1A EP3428144A1 (fr) 2017-07-12 2017-07-12 Procédé et installation de fabrication de propylène par combinaison de déshydrogénation de propane et procédé de vapocraquage avec recyclage de propane au procédé de vapocraquage
EP17180984.1 2017-07-12
PCT/EP2018/068967 WO2019012051A1 (fr) 2017-07-12 2018-07-12 Procédé et installation pour la production de propylène par combinaison d'une déshydrogénation de propane et d'un procédé de vapocraquage avec recyclage du propane dans le procédé de vapocraquage

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Cited By (2)

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Publication number Priority date Publication date Assignee Title
US11198661B2 (en) * 2019-09-10 2021-12-14 Kellogg Brown & Root Llc Process for recovery of propylene from a propane dehydrogenation process
WO2024112883A1 (fr) * 2022-11-23 2024-05-30 Uop Llc Récupération de produit de déshydrogénation et de pyrolyse avec un déméthaniseur commun

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US4458096A (en) 1983-05-26 1984-07-03 Air Products And Chemicals, Inc. Process for the production of ethylene and propylene
DE102005053732A1 (de) * 2005-11-10 2007-05-16 Linde Ag Verfahren zur Erhöhung der Propylenausbeute in Ethylenanlagen
US8563793B2 (en) 2009-06-29 2013-10-22 Uop Llc Integrated processes for propylene production and recovery
CN102320912B (zh) * 2011-06-03 2014-04-16 神华集团有限责任公司 最大化含氧化合物转化制备低碳烯烃工艺中的乙烯和丙烯总收率的方法
CN103086826B (zh) * 2011-10-28 2015-09-16 中国石油化工股份有限公司 一种乙烯和丙烯的联产方法
KR102374392B1 (ko) * 2014-02-25 2022-03-15 사빅 글로벌 테크놀러지스 비.브이. 탄화수소를 올레핀으로 전환하는 공정
CN104151121B (zh) * 2014-08-13 2016-01-20 中石化上海工程有限公司 Mto工艺与石脑油裂解前脱丙烷工艺耦合的方法

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11198661B2 (en) * 2019-09-10 2021-12-14 Kellogg Brown & Root Llc Process for recovery of propylene from a propane dehydrogenation process
US20220041528A1 (en) * 2019-09-10 2022-02-10 Kellogg Brown & Root Llc. System for recovery of propylene from a propane dehydrogenation process
US11548843B2 (en) * 2019-09-10 2023-01-10 Kellogg Brown & Root Llc System for recovery of propylene from a propane dehydrogenation process
WO2024112883A1 (fr) * 2022-11-23 2024-05-30 Uop Llc Récupération de produit de déshydrogénation et de pyrolyse avec un déméthaniseur commun

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EP3428144A1 (fr) 2019-01-16
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AU2018300036A1 (en) 2020-01-16
CN110914225A (zh) 2020-03-24
ES2895637T3 (es) 2022-02-22
AU2018300036B2 (en) 2022-08-04
RU2020101585A3 (fr) 2022-03-10
WO2019012051A1 (fr) 2019-01-17
RU2020101585A (ru) 2021-08-12
KR20200026946A (ko) 2020-03-11
PH12019502862A1 (en) 2020-10-05

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